EP4355706B1 - Installation de clinker de ciment et procédé de dépôt d'un constituant volatil - Google Patents

Installation de clinker de ciment et procédé de dépôt d'un constituant volatil

Info

Publication number
EP4355706B1
EP4355706B1 EP22741687.2A EP22741687A EP4355706B1 EP 4355706 B1 EP4355706 B1 EP 4355706B1 EP 22741687 A EP22741687 A EP 22741687A EP 4355706 B1 EP4355706 B1 EP 4355706B1
Authority
EP
European Patent Office
Prior art keywords
mobile container
flue gases
sorbent
installation
container
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
EP22741687.2A
Other languages
German (de)
English (en)
Other versions
EP4355706A1 (fr
EP4355706C0 (fr
Inventor
Thomas Fellner
Manuel DREXLER
Markus STECHER
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Scheuch Management Holding GmbH
Original Assignee
Scheuch Management Holding GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Scheuch Management Holding GmbH filed Critical Scheuch Management Holding GmbH
Publication of EP4355706A1 publication Critical patent/EP4355706A1/fr
Application granted granted Critical
Publication of EP4355706B1 publication Critical patent/EP4355706B1/fr
Publication of EP4355706C0 publication Critical patent/EP4355706C0/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/64—Heavy metals or compounds thereof, e.g. mercury
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B7/00—Hydraulic cements
    • C04B7/36—Manufacture of hydraulic cements in general
    • C04B7/364—Avoiding environmental pollution during cement-manufacturing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B01D2257/602—Mercury or mercury compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0233—Other waste gases from cement factories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/45—Gas separation or purification devices adapted for specific applications
    • B01D2259/455—Gas separation or purification devices adapted for specific applications for transportable use
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides

Definitions

  • the invention relates to a plant, in particular a cement clinker plant, for separating a volatile component, in particular mercury, from flue gases, comprising: a mobile container with a supply line and a discharge line for the flue gases, whereby the mobile container is designed as a transportable swap body.
  • the invention relates to a process for separating a volatile component, in particular mercury, from flue gases, in particular from cement clinker production.
  • EP 2 892 861 describes how mercury is introduced into the cement clinker production process via the raw materials.
  • the raw materials for cement clinker production are passed through a preheater, exchanging heat with the kiln exhaust gases, and then fired in a rotary kiln. Heating the raw materials in the preheater evaporates the mercury bound in the raw materials.
  • a portion of the flue gases is first dedusted using a hot gas filter and then brought to a temperature below 250°C using an evaporative cooler.
  • a sorbent such as activated carbon is then injected into the flue gases, to which the mercury is bound.
  • the activated carbon is separated using a bag filter.
  • the cleaned flue gas can then be returned to the process.
  • the EP 2 892 861 Furthermore, it has already been mentioned that the mercury can be separated from the flue gases using a fixed or moving bed adsorber.
  • KR200410276 discloses a system for reducing emissions from exhaust gases.
  • the dry emission control system is based on the adsorption of ionic mercury compounds using a fixed-bed adsorber, for example, based on a mixture of granular activated carbon or furnace coke.
  • a dust collector is installed in the tube furnace.
  • the object of the invention is therefore to alleviate or eliminate at least some of the disadvantages of the prior art.
  • the invention preferably aims to create a structurally simple and operationally reliable system and a corresponding method for the separation of volatile components such as mercury from flue gases. This object is achieved by a system according to claim 1 and a method according to claim 11. Preferred embodiments are specified in the dependent claims.
  • the mobile container contains several containers each filled with a fixed bed of a sorbent, in particular of a carbonaceous and/or mineral sorbent, and the mobile container has a bracket for attaching a lifting device.
  • the flue gases are thus freed of the volatile component, in particular mercury, with the aid of a fixed bed adsorber.
  • a preferably cuboid-shaped mobile or interchangeable container is provided as the fixed bed adsorber, in the interior of which several, in particular more than 5, preferably more than 10, for example more than 15, containers are arranged, each containing the fixed bed of the sorbent. Due to the fixed bed design, the sorbent is arranged stationary (i.e. immobile) during the separation of the volatile component. To reduce operating problems such as self-ignition, the sorbent is distributed among the individual containers in the mobile container.
  • the temperature of the flue gas in the containers can thus be more than 40 °C, in particular more than 50 °C and preferably less than 210 °C, in particular less than 200 °C, without having to increase the fire protection measures.
  • a carbon-containing sorbent in particular pure activated carbon, in particular brominated activated carbon, can be provided as the sorbent.
  • a mixture of activated carbon and minerals, such as lime, can be used as the sorbent.
  • the volatile component in particular gaseous mercury
  • the fixed-bed adsorber mobile container is free of any conveying device, such as a rotary valve, for the sorbent.
  • the containers can be sealed essentially hermetically for the exchange of the sorbent. In the hermetically sealed state, the containers containing the loaded sorbent can be replaced with containers containing unloaded sorbent. This exchange can take place, for example, once a year. This also includes external disposal and treatment by qualified personnel.
  • the mobile container is designed as a transportable swap body.
  • the mobile container has a mounting bracket, for example, an eyelet, for attaching a lifting device, such as a crane.
  • a mounting bracket for example, an eyelet
  • several, in particular four, mounting brackets, in particular eyelets, are provided.
  • the mounting brackets are preferably designed so that the total weight of the mobile container with the containers can be supported by the mounting brackets.
  • the containers each have a perforated bottom, in particular a perforated plate, with first openings on the underside through which the flue gases can flow.
  • the containers can each have a perforated lid, in particular a further perforated plate, on the top side through which the flue gases can flow.
  • the capacity of the containers is preferably less than 300 liters (l), in particular less than 250 l, preferably less than 220 l . Furthermore, it is preferred if the capacity of the containers (and thus the volume of the respective fixed bed) is more than 100 liters, preferably more than 150 liters. For example, the capacity of the containers is substantially 200 l .
  • the system comprises a further mobile container with a further supply line for flue gases to be freed from the volatile components and a further discharge line for flue gases freed from the volatile components, wherein further containers, each filled with a sorbent, are arranged in the further mobile container.
  • further containers each filled with a sorbent
  • (at least) two mobile containers are provided, each with several containers for the sorbent. This allows the separation efficiency to be increased. It is particularly advantageous that in this series connection, the Sorption potential can be exploited to the end, ie until breakthrough.
  • the mobile container and the additional mobile container can be connected in series, with the mobile container's outlet connected to the additional supply line of the additional mobile container.
  • the flue gases are first directed through the containers in the mobile container and then through the additional containers in the additional mobile container. This increases the separation efficiency for the volatile component, especially mercury.
  • the mobile container and the additional mobile container can be connected in parallel, whereby the flue gases to be freed of the volatile component can be fed optionally to the supply line of the mobile container or the additional supply line of the additional mobile container.
  • the mobile container can be removed from the system in order to replace the fixed bed of sorbent loaded with the volatile component with an unloaded sorbent free of volatile component.
  • the system does not have to be shut down to replace the sorbent.
  • the mobile container can be disconnected from the supply and discharge lines.
  • the supply and discharge lines can each be blocked with a blind flange.
  • a crane can be used to remove the mobile container; in a preferred embodiment, this crane is connected to the holder.
  • the containers can then be disposed of.
  • the mobile container is then refilled with fresh containers.
  • the flue gas can be routed through the other containers within the additional mobile container.
  • the sorbent in the other containers of the additional mobile container is exchanged accordingly.
  • the additional mobile container with the additional containers is preferably identical to the mobile container with the containers. All preferred design variants of the mobile container can equally refer to the additional mobile container with the additional containers.
  • the container is preferably a barrel, in particular with a capacity of more than 100 liters, preferably more than 150 liters, for example, essentially 200 liters.
  • the barrel preferably has a circular cross-section.
  • the mobile container is preferably designed as a cuboid with a length, a width and a height, wherein the length is preferably greater, in particular several times greater, than the width of the mobile container.
  • the mobile container has a length of 5 meters (m) to 13 m, in particular substantially 12 m, a width of 2 m to 3 m, in particular substantially 2.5 m, and a height of 1.5 m to 3 m, in particular substantially 2 m.
  • rows in particular at least three rows, each with several, in particular with more than three, for example with more than five, containers are provided in the interior of the mobile container.
  • the mobile container preferably has an intermediate floor with passage openings, above which the containers containing the sorbent are arranged, in particular positioned.
  • the intermediate floor preferably extends parallel to a floor of the mobile container.
  • the intermediate floor is preferably arranged closer to the floor than to a ceiling of the mobile container.
  • the containers preferably have openings on the underside through which the flue gases enter the respective fixed bed of sorbent.
  • the supply and discharge lines are preferably arranged so that the containers inside the mobile container are arranged from bottom to are flowed through by the flue gases at the top.
  • location references such as “above,” “below,” “horizontal,” and “vertical” refer to the intended arrangement of the system, in particular the mobile container, on a horizontal surface.
  • Directional references such as “before” and “after” refer to the flow direction of the flue gases.
  • a dust filter in particular a hot gas filter, is preferably arranged in front of the mobile container.
  • the hot gas filter is designed to dedust the flue gases at a temperature of more than 250 °C.
  • the dust separated by the hot gas filter can be recirculated. If the plant is designed as a cement clinker plant, the dust can be recirculated to the preheater.
  • a cooler in particular an evaporative cooler or a heat exchanger, is arranged between the dust filter and the mobile container.
  • the flue gases can be cooled to the temperature required for the separation of the volatile components, in particular less than 210°C, for example to 50 to 200°C.
  • the exhaust gas stream is cooled by injecting very fine water droplets into the hot exhaust gas stream. The evaporation process extracts heat from the flue gases and reaches the desired temperature level for the subsequent exhaust gas purification.
  • the design of the cooler as a heat exchanger is particularly advantageous. This avoids the disadvantages of an evaporative cooler, which in particular consist in the potential for clumping during the process.
  • acidic gas components can react with the water from the quench, creating an acidic environment that has a highly corrosive effect.
  • the device can comprise a heat exchanger upstream of the mobile container and another heat exchanger downstream of the mobile container.
  • a heat transfer medium can be routed between the heat exchanger and the additional heat exchanger.
  • SCR Selective Catalytic Reduction
  • the SCR module can also serve to minimize the ammonia concentration in the flue gas. The ammonia is adsorbed by the activated carbon and neutralizes it. This would result in poorer adsorption of mercury, which requires an acidic environment for adsorption.
  • the flue gases can be passed through another mobile container after flowing through the mobile container, in which further containers are arranged, each filled with a sorbent, in particular a carbon-containing and/or mineral sorbent.
  • the flue gases for exchanging the loaded sorbent in the containers of the mobile container can be led exclusively through the other containers of the other mobile container.
  • the method may further comprise the following step: Dust removal from the flue gases, particularly with a hot gas filter, before feeding the flue gases into the mobile container.
  • Fig. 1 is a schematic view of a cement clinker plant 1 for producing cement clinker from raw material, in particular Raw meal, shown.
  • Plant 1 has a conventional plant design, symbolized here by field 2.
  • This plant design 2 includes a (rotary) kiln, which can be connected to a clinker cooler on the one hand and to a preheating stage on the other.
  • the preheating stage can have a cyclone cascade with several cyclones, with which the raw material is preheated.
  • the raw material can be fed into the uppermost cyclone of the preheating stage via a material feeder.
  • the preheated raw material enters the rotary kiln, in which the raw material is burned to produce cement clinker.
  • the kiln exhaust gases or flue gases produced during combustion are passed through the preheating stage against the flow of the raw material.
  • the plant can also have a calciner.
  • the cement clinker plant 1 can also have a raw mill, in which the raw material can be ground and, in particular, dried with the help of the flue gases.
  • Flue gases are extracted from the plant structure 2, in particular from the preheating stage or from the calciner (see arrow 3).
  • the flue gases are fed to a dust filter 4, here a hot gas filter.
  • the hot gas filter has at least one filter element, preferably several filter elements, in particular filter candles, preferably made of ceramic or metal, on which the dust from the flue gases is separated.
  • the separated dust can be fed into the preheater or fed to a silo (see arrow 5).
  • the flue gases are then cooled to temperatures of 50 to 200 °C with the aid of a cooler, here designed as a heat exchanger 6, in order to enable the separation of a volatile component, in particular mercury, from the flue gases.
  • the heat from the flue gases absorbed by the heat exchanger 6 can be used elsewhere in the cement clinker plant 1.
  • the dedusted and cooled flue gases are conveyed to a mobile container 7 with a supply line 7A and a discharge line 7B for flue gases to separate the volatile components. Finally, the flue gases freed from volatile components can be fed to an exhaust gas purification system 10.
  • the mobile container 7 for the reduction of the volatile component in the flue gases is in the Fig. 2 and 3 presented in detail.
  • the mobile container 7 is cuboid-shaped with a length, a width, and a height, wherein the length is preferably greater than the width.
  • a plurality of containers 8 Arranged inside the mobile container 7 are a plurality of containers 8, each filled with a fixed bed 9, i.e. with a stationary arrangement, in particular a bed, of preferably carbon-containing sorbent, also referred to as sorption agent. Barrels with a circular cross-section can be provided as containers 8.
  • the capacity of the barrels can, for example, be substantially 200 liters.
  • the mobile container 7 has a floor 11A, side walls 11B, and a ceiling 11C.
  • struts 12 are provided, preferably at least on the side walls 11B and the ceiling 11C.
  • an intermediate floor 13 is arranged closer to the floor 10 than to the ceiling 12.
  • the containers 8 stand on the intermediate floor 13.
  • Through-openings 14 are formed on the intermediate floor 13, above which the containers 8 containing the carbon-containing sorbent are arranged.
  • the containers 8 have a perforated floor, in particular a perforated plate, on their underside with openings through which the flue gases can enter. This allows the flue gases to flow from a space 15 below the intermediate floor 13 through the through-openings 14 into the containers 8. With the aid of the carbon-containing sorbent, the proportion of volatile components, in particular mercury, in the flue gases is reduced. After passing through the containers 8, the flue gases are withdrawn from the space 17 above the intermediate floor 13 via the discharge line 7B, which may have at least one pipe 16.
  • FIG. 4 An alternative system diagram is shown, whereby only the differences are pointed out below. Fig. 1 to 3 should be addressed.
  • the flue gases are also initially fed to a dust filter 4, where dust essentially free of mercury is separated and then, for example, returned to the preheating stage (see arrow 18).
  • the flue gases are then fed, for example at essentially 350°C, to an SCR module 19, which is designed for the selective catalytic reduction of nitrogen compounds ("denitrification").
  • SCR module 19 which is designed for the selective catalytic reduction of nitrogen compounds ("denitrification").
  • the flue gases Upstream of the mobile container 7, the flue gases are fed to the heat exchanger 6, which, together with another heat exchanger 20 downstream of the mobile container 7, forms a device 21 for transferring heat from the flue gases upstream of the mobile container 7 to the flue gases downstream of the mobile container 7.
  • the appropriate temperature level in particular 50 to 200°C, is maintained for the separation of the volatile component in the mobile container 7, and at the same time, the heat content of the flue gases is recovered.
  • a heat exchange medium can be guided between the heat exchanger 6 and the further heat exchanger 20, which absorbs the heat from the flue gases in front of the mobile container at the heat exchanger 6 and transfers the heat to the flue gases at the further heat exchanger 20.
  • the heat absorbed by the heat exchanger 6 can also be transferred to another location in the cement clinker production process.
  • the flue gases are fed to the exhaust gas purification system 10 or returned to the process.
  • a further mobile container 22 is provided with a further supply line 23 and a further discharge line 24 for the flue gases.
  • the further mobile container 22 is identical to the mobile container 7. Accordingly, further containers are arranged inside the further mobile container 22, each filled with a carbon-containing sorbent.
  • the mobile container 7 and the further mobile container 22 can be flowed through individually or one after the other.
  • the mobile container 7 and the further mobile container 22 are connected in series, with the discharge line 7B of the mobile container 7 being connected to the further supply line 23 of the further mobile container 22.
  • the entire flue gas can be passed first through the mobile container 7 and then through the further mobile container 22.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Ceramic Engineering (AREA)
  • Biomedical Technology (AREA)
  • Ecology (AREA)
  • Structural Engineering (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Public Health (AREA)
  • Environmental Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Treating Waste Gases (AREA)

Claims (14)

  1. Installation, en particulier installation de clinker de ciment (1), pour la séparation d'un composant volatil, en particulier du mercure, des gaz de fumée, comprenant :
    un conteneur mobile (7) avec une conduite d'amenée (7A) et une conduite d'évacuation (7B) pour les gaz de fumée, le conteneur mobile (7) étant conçu comme un récipient interchangeable transportable,
    caractérisée en ce que
    dans le conteneur mobile (7) sont disposés plusieurs récipients (8) chacun rempli d'un lit fixe (9) d'un sorbant, en particulier un sorbant carboné et/ou minéral, le conteneur mobile (7) comprenant un support pour la fixation d'un dispositif de levage.
  2. Installation (1) selon la revendication 1, caractérisée par
    un autre conteneur mobile (22) avec une autre conduite d'amenée (23) et une autre conduite d'évacuation (24) pour les gaz de fumée, dans lequel d'autres récipients chacun rempli d'un sorbant sont disposés dans l'autre conteneur mobile (22).
  3. Installation (1) selon la revendication 2, caractérisée en ce que le conteneur mobile (7) et l'autre conteneur mobile (22) sont connectés en série dans une première position de commutation, la conduite d'évacuation (7B) du conteneur mobile (7) étant reliée à l'autre conduite d'amenée (23) de l'autre conteneur mobile (22).
  4. Installation (1) selon la revendication 2 ou 3, caractérisée en ce que le conteneur mobile (7) et l'autre conteneur mobile (22) sont connectés en parallèle dans une deuxième position de commutation, les gaz de fumée pouvant être amenés au choix à la conduite d'amenée (7A) du conteneur mobile (7) ou à l'autre conduite d'amenée de l'autre conteneur mobile (22).
  5. Installation (1) selon l'une des revendications 1 à 4, caractérisée en ce que chaque récipient (8) est prévu sous forme de fût, en particulier avec une capacité de plus de 100 litres, de préférence de plus de 150 litres, et de préférence de moins de 300 litres, particulièrement de préférence de moins de 250 litres, par exemple essentiellement de 200 litres.
  6. Installation (1) selon l'une des revendications 1 à 5, caractérisée en ce que le conteneur mobile (22) comprend un plancher intermédiaire (13) avec des ouvertures de passage (14), au-dessus desquelles sont disposés les récipients (8) avec le sorbant.
  7. Installation (1) selon l'une des revendications 1 à 6, caractérisée en ce qu'un filtre à poussière (4), en particulier un filtre à gaz chaud, est disposé avant le conteneur mobile (7).
  8. Installation (1) selon la revendication 7, caractérisée en ce qu'un refroidisseur, en particulier un refroidisseur par évaporation ou un échangeur de chaleur, est disposé entre le filtre à poussière (4) et le conteneur mobile (7).
  9. Installation (1) selon l'une des revendications 1 à 8, caractérisée en ce qu'un dispositif (21) est prévu pour transférer la chaleur des gaz de fumée avant le conteneur mobile (7) aux gaz de fumée après le conteneur mobile (7).
  10. Installation (1) selon l'une des revendications 7 à 9, caractérisée en ce qu'un module SCR est disposé entre le filtre à poussière (4) et le conteneur mobile (22).
  11. Procédé de séparation d'un composant volatil, en particulier du mercure, des gaz de fumée, en particulier de la production de clinker de ciment, comprenant les étapes suivantes :
    amenée des gaz de fumée dans un conteneur mobile (7), dans lequel sont disposés plusieurs récipients (8) remplis d'un lit fixe (9) d'un sorbant, en particulier un sorbant carboné et/ou minéral, le conteneur mobile (7) étant conçu comme un récipient interchangeable transportable ;
    séparation du composant volatil des gaz de fumée sur le sorbant dans les récipients (8) ; et
    évacuation des gaz de fumée du conteneur mobile (7).
  12. Procédé selon la revendication 11, caractérisé en ce que les gaz de fumée, après avoir traversé le conteneur mobile (7), sont dirigés à travers un autre conteneur mobile (22), dans lequel d'autres récipients chacun rempli d'un sorbant sont disposés.
  13. Procédé selon la revendication 12, caractérisé en ce que les gaz de fumée, pour remplacer le sorbant chargé dans les récipients (8) du conteneur mobile (7), sont dirigés exclusivement à travers les autres récipients (8) de l'autre conteneur mobile (22) .
  14. Procédé selon la revendication 12 ou 13, caractérisé en ce que
    le dépoussiérage des gaz de fumée, en particulier avec un filtre à gaz chaud, avant l'amenée des gaz de fumée dans le conteneur mobile (7).
EP22741687.2A 2021-06-15 2022-06-14 Installation de clinker de ciment et procédé de dépôt d'un constituant volatil Active EP4355706B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA50480/2021A AT524447B1 (de) 2021-06-15 2021-06-15 Zementklinkeranlage und Verfahren zur Abscheidung eines flüchtigen Bestandteils
PCT/AT2022/060195 WO2022261686A1 (fr) 2021-06-15 2022-06-14 Installation de clinker de ciment et procédé de dépôt d'un constituant volatil

Publications (3)

Publication Number Publication Date
EP4355706A1 EP4355706A1 (fr) 2024-04-24
EP4355706B1 true EP4355706B1 (fr) 2025-08-06
EP4355706C0 EP4355706C0 (fr) 2025-08-06

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EP22741687.2A Active EP4355706B1 (fr) 2021-06-15 2022-06-14 Installation de clinker de ciment et procédé de dépôt d'un constituant volatil

Country Status (3)

Country Link
EP (1) EP4355706B1 (fr)
AT (1) AT524447B1 (fr)
WO (1) WO2022261686A1 (fr)

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AT524447A4 (de) 2022-06-15
EP4355706A1 (fr) 2024-04-24
AT524447B1 (de) 2022-06-15
EP4355706C0 (fr) 2025-08-06

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